WO2013032537A1 - Processus de fonctionnement de procédé de production de gaz de synthèse à partir de matière carbonée - Google Patents

Processus de fonctionnement de procédé de production de gaz de synthèse à partir de matière carbonée Download PDF

Info

Publication number
WO2013032537A1
WO2013032537A1 PCT/US2012/032168 US2012032168W WO2013032537A1 WO 2013032537 A1 WO2013032537 A1 WO 2013032537A1 US 2012032168 W US2012032168 W US 2012032168W WO 2013032537 A1 WO2013032537 A1 WO 2013032537A1
Authority
WO
WIPO (PCT)
Prior art keywords
syngas
carbonaceous material
cooled
produce
cooler
Prior art date
Application number
PCT/US2012/032168
Other languages
English (en)
Inventor
Ching-Whan Ko
Michael Sean Slape
Peter S BELL
Kim OCFEMIA
Original Assignee
Ineos Bio Sa
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to AU2012302236A priority Critical patent/AU2012302236B2/en
Priority to MX2013011708A priority patent/MX2013011708A/es
Priority to JP2014503951A priority patent/JP6127323B2/ja
Priority to EP12715788.1A priority patent/EP2694624B1/fr
Application filed by Ineos Bio Sa filed Critical Ineos Bio Sa
Priority to BR112013025718A priority patent/BR112013025718B1/pt
Priority to CN201280024944.1A priority patent/CN103874750B/zh
Priority to EP18203543.6A priority patent/EP3453747A1/fr
Priority to EA201370217A priority patent/EA029848B1/ru
Priority to CA2832431A priority patent/CA2832431C/fr
Priority to KR1020137029101A priority patent/KR101882544B1/ko
Priority to ES12715788T priority patent/ES2708221T3/es
Priority to PL12715788T priority patent/PL2694624T3/pl
Priority to NZ617115A priority patent/NZ617115B2/en
Publication of WO2013032537A1 publication Critical patent/WO2013032537A1/fr
Priority to ZA2013/08269A priority patent/ZA201308269B/en

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/726—Start-up
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/86—Other features combined with waste-heat boilers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/005—Reducing the tar content by partial oxidation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/008—Reducing the tar content by cracking
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • F22B1/1838—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines the hot gas being under a high pressure, e.g. in chemical installations
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0877—Methods of cooling by direct injection of fluid
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0888—Methods of cooling by evaporation of a fluid
    • C01B2203/0894—Generation of steam
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • C01B2203/143—Three or more reforming, decomposition or partial oxidation steps in series
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/32—Hydrogen storage
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/12—Improving ICE efficiencies

Definitions

  • a process for gasification of carbonaceous materials to produce producer gas or synthesis gas or syngas comprising carbon monoxide and hydrogen. More specifically, the process is effective for producing cooled syngas for downstream use.
  • the process utilizes gasification of carbonaceous materials to produce a syngas followed by cooling of said syngas to produce cooled syngas and optionally cleaning said cooled syngas to produce a clean syngas for several downstream processes.
  • Gasification of carbonaceous materials to produce producer gas or synthesis gas or syngas comprising carbon monoxide and hydrogen is well known in the art.
  • a gasification process involves a partial oxidation or starved-air oxidation of carbonaceous material in which a sub-stoichiometric amount of oxygen is supplied to the gasification process to promote production of carbon monoxide as disclosed in PCT Patent Application No. WO 93/018341.
  • Gaseous products produced by partial oxidation of carbonaceous materials are often treated in a high temperature heat treatment unit, e.g. for destruction of tar.
  • WO 2009/154788 discloses a two stage gasifier in which carbonaceous material is fed to the first stage in which air, oxygen-enriched air or pure oxygen can be injected at controlled rate.
  • the first stage temperature and oxygen input is controlled such that only partial oxidation of carbonaceous material occurs.
  • the gaseous product from the first stage moves to the second stage (heat treatment unit). Pure oxygen is introduced into the second stage in order to accomplish cracking and partial oxidation of any tar contained in the gaseous stream from the first stage.
  • Product syngas is removed from the second stage.
  • Hot syngas produced by gasification processes described in the art can be hot and needs cooling prior to downstream processing. Recovery and use of this heat content of hot syngas can be very important for process economics.
  • Hot syngas comprising carbon monoxide generated in gasification apparatus is cooled in a heat exchanger or waste heat boiler downstream of the gasification apparatus. See for example US Patent No. 6,435, 139; US Patent No. 7,587,995 and US Patent No. 7,552,701.
  • carbon monoxide At high temperature reducing environment carbon monoxide is a stable product. However when carbon monoxide is cooled, carbon monoxide may oxidize into carbon dioxide, and produce carbon (graphite) that precipitates as soot:
  • This reaction is generally known as Boudouard reaction and is believed to take place at or below about 760°C. Fouling of heat transfer surface caused by deposit of carbon can cause disruption in operation of a syngas cooler. It is, therefore, important to eliminate or reduce fouling of the syngas cooler.
  • Sulfur in carbonaceous matter transforms to 3 ⁇ 4S in reductive mode of operation, to SO2 in oxidative mode of operation. It is advantageous to make S0 2 during start-up so that it can be scrubbed easily prior to disposal.
  • a process for producing syngas that is effective for use in downstream processes includes operating a gasification apparatus in a start-up mode until the gasification apparatus and equipment downstream of the gasification apparatus are adequately warmed up to a first target temperature. Upon reaching a first target temperature, the process is then operated in a production mode to produce a second syngas with a higher CO/CO2 molar ratio. Operation in a start-up mode until reaching a first target temperature provides a process that is effective for reducing fouling in downstream equipment and for providing a second syngas can be more effectively cooled and cleaned.
  • the second syngas with a higher CO/C0 2 molar ratio that is cooled and cleaned is especially useful for fermentation processes.
  • the process for producing syngas includes gasifying carbonaceous material to provide a first syngas having a CO to C0 2 molar ratio of less than about 0.5 until the first syngas reaches a first target temperature. Upon reaching the first target temperature, carbonaceous material is gasified to provide a second syngas having a CO to C0 2 molar ratio of greater than the first syngas. Gasifying of carbonaceous materia! occurs in a gasification apparatus and molecular oxygen is introduced at a rate of about 0 to about 100 lb-mole per ton of carbonaceous material on a dry basis to provide the first syngas. The temperature of the first syngas may be measured at one or more points inside and/or downstream of the gasification apparatus.
  • the temperature of the first syngas at one or more points inside and/or outside the gasification apparatus reaches the first target temperature
  • molecular oxygen is introduced at a rate of a rate of 0 to about 100 lb-mole per ton of carbonaceous material on a dry basis to provide the second syngas.
  • the first target temperature is about 700° C to about 1000°C.
  • At least a portion of the first syngas is passed through a syngas cooler to produce a cooled first syngas and at least a portion of the second syngas is passed through a syngas cooler to produce a cooled second syngas.
  • syngas is passed through the syngas cooler at a linear velocity of greater than about 24 meters per second.
  • At least a portion of the first syngas is provided to a thermal oxidation unit until the first syngas reaches the first target temperature.
  • a process is provided to produce syngas that includes adding carbonaceous material and molecular oxygen to a gasification apparatus to produce a first syngas with CO/C0 2 molar ratio less than 0.5.
  • the temperature of the first syngas is measured downstream of the gasification apparatus. Temperature may be measured prior to entry into a syngas cooler or downstream of a syngas cooler. Once the syngas reaches a first temperature prior to entry into a syngas cooler, addition of molecular oxygen is reduced per unit mass of carbonaceous material in the gasification apparatus to produce a second syngas with CO/C0 2 molar ratio greater than that of said first syngas.
  • the first target temperature is about 700°C to about 1000°C.
  • Reduction of addition of molecular oxygen per unit mass of carbonaceous material may be accomplished by increasing rate of addition of carbonaceous material.
  • reduction of addition of molecular oxygen per unit mass of carbonaceous material may be accomplished by decreasing rate of addition of molecular oxygen.
  • At least a portion of the first syngas may be passed through the syngas cooler to produce a cooled first syngas and at least a portion of the second syngas may be passed through a syngas cooler to produce a cooled second syngas.
  • At least a portion of the cooled first syngas may be mixed with a portion of the first syngas prior to its passing through said syngas cooler to produce the cooled first syngas.
  • At least a portion of the cooled second syngas may be mixed with at least a portion of the second syngas prior to passing through the syngas cooler to produce the cooled second syngas.
  • the mixture of the cooled first syngas and the first syngas flowing through the syngas cooler may have a linear velocity of greater than about 24 meter/second.
  • the mixture of the cooled second syngas and the second syngas flowing through the syngas cooler may have a linear velocity of greater than about 24 meter/second.
  • one or more of steam and CO2 may be added to the gasification apparatus prior to reduction of the addition of molecular oxygen per unit mass of carbonaceous material or prior to reaching a first target temperature.
  • first target temperature less than about 50 lb-mole steam per ton of carbonaceous material on a dry basis or less than about 50 lb-mole CO2 per ton of carbonaceous material on a dry basis is added.
  • a process in another aspect, includes gasifying carbonaceous material in a gasification apparatus to produce a clean syngas.
  • the method includes adding carbonaceous material and adding molecular oxygen in the gasification apparatus to produce a first syngas with CO/CO2 molar ratio less than 0.5. At least a portion of the first syngas is passed through the syngas cooler to produce a cooled first syngas. At least a portion of the first cooled syngas is passed through a dust collection system to produce a clean syngas. The temperature of the clean syngas is measured at an exit of the dust collection system.
  • the second target temperature is about 100°C to about 200°C.
  • the process is effective for providing a syngas having less than about 10 ppm tars.
  • a process for cooling syngas.
  • the process includes passing a syngas through a syngas cooler to produce a cooled syngas; and recycling at least a portion of the cooled syngas to an inlet of the syngas cooler to maintain a temperature at the inlet of the syngas cooler of 760°C or less and a linear velocity through the syngas cooler of at least 24 meters per second.
  • Figure 1 is a schematic diagram of an aspect of a process that includes gasification of carbonaceous material by treating with molecular oxygen in a gasification apparatus to produce a hot syngas and subsequent cooling of said hot syngas in a syngas cooler to produce a cooled syngas.
  • Figure 2 is a schematic diagram of an aspect of a process that includes gasification of carbonaceous material by treating with molecular oxygen in a gasification apparatus to produce a hot syngas and subsequent cooling of said hot syngas in a syngas cooler to produce a cooled syngas; wherein at least a part of said cooled syngas is recycled and mixed with said hot syngas prior to entry into syngas cooler.
  • Figure 3 is a schematic diagram of an aspect of a process that includes gasification of carbonaceous material by treating with molecular oxygen in a gasification apparatus to produce a hot syngas and subsequent cooling of said hot syngas in a syngas cooler to produce a cooled syngas; wherein at least a part of said cooled syngas is recycled and mixed with said hot syngas prior to entry into syngas cooler; and wherein the gasification apparatus includes two reaction zones, e.g., a gasification zone and a heat treatment zone connected through a connecting zone.
  • Figure 4 is a schematic diagram of an aspect of a process that includes gasification of carbonaceous material by treating with molecular oxygen in a gasification apparatus to produce a hot syngas and subsequent cooling of said hot syngas in a syngas cooler to produce a cooled syngas; wherein at least a part of said cooled syngas is recycled and mixed with said hot syngas prior to entry into syngas cooler; wherein at least a portion of one or more of hot and cooled syngas can be sent to a thermal oxidation unit; and wherein at least a portion of said cooled syngas can be processed in a bag-house.
  • any amount refers to the variation in that amount encountered in real world conditions, e.g., in the lab, pilot plant, or production facility.
  • an amount of an ingredient or measurement employed in a mixture or quantity when modified by “about” includes the variation and degree of care typically employed in measuring in an experimental condition in production plant or lab.
  • the amount of a component of a product when modified by “about” includes the variation between batches in a multiple experiments in the plant or lab and the variation inherent in the analytical method. Whether or not modified by “about,” the amounts include equivalents to those amounts. Any quantity stated herein and modified by “about” can also be employed in the present disclosure as the amount not modified by "about”.
  • bag-house or “baghouse” means process or equipment designed for the use of engineered fabric filter tubes, envelopes or cartridges for capturing, separation or filtering of solid particles (fine particles, dust) contained in a gas. Dust-laden or solid- laden gases enter the bag-house and pass through fabric bags that act as filters.
  • the bags can be of woven or felted cotton, synthetic, or glass-fiber material in either a tube or envelope shape. Common types of bag-houses include mechanical shaker, reverse air, and reverse jet.
  • Carbonaceous material refers to carbon rich material such as coal, and petrochemicals.
  • carbonaceous material includes any carbon material whether in solid, liquid, gas, or plasma state.
  • the present disclosure contemplates: carbonaceous material, carbonaceous liquid product, carbonaceous industrial liquid recycle, carbonaceous municipal solid waste (MSW or msw), carbonaceous urban waste, carbonaceous agricultural material, carbonaceous forestry material, carbonaceous wood waste, carbonaceous construction material, carbonaceous vegetative material, carbonaceous industrial waste, carbonaceous fermentation waste, carbonaceous petrochemical co products, carbonaceous alcohol production co-products, carbonaceous coal, tires, plastics, waste plastic, coke oven tar, fibersoft, lignin, black liquor, polymers, waste polymers, polyethylene terephthalate (PETA), polystyrene (PS), sewage sludge, animal waste, crop residues, energy crops, forest processing residue
  • dust collector or “dust collection system” means process or equipment designed for capturing, separation or filtering of solid particles (fine particles, dust) contained in a gas.
  • a dust collection system generally consists of a blower, dust filter, a filter-cleaning system, and a dust receptacle or dust removal system.
  • Principal types of industrial dust collectors include inertial separators, fabric filters or bag-houses, wet scrubbers, electrostatic precipitators, and unit collectors.
  • fibersoft or “Fibersoft” or “fibrosoft” or “fibrousoft” means a type of carbonaceous material that is produced as a result of softening and concentration of various substances; in an example carbonaceous material is produced via steam autoclaving of various substances.
  • the fibersoft can include steam autoclaving of municipal, industrial, commercial, and medical waste resulting in a fibrous mushy material.
  • municipal solid waste or "MSW” or “msw” means waste that may include household, commercial, industrial and/or residual waste.
  • Syngas means synthesis gas which is the name given to a gas mixture that contains varying amounts of carbon monoxide and hydrogen.
  • Examples of production methods include steam reforming of natural gas or hydrocarbons to produce hydrogen, the gasification of coal and in some types of waste-to-energy gasification facilities. The name comes from their use as intermediates in creating synthetic natural gas (SNG) and for producing ammonia or methanol.
  • Syngas comprises use as an intermediate in producing synthetic petroleum for use as a fuel or lubricant via Fischer-Tropsch synthesis and previously the Mobil methanol to gasoline process.
  • Syngas consists primarily of hydrogen, carbon monoxide, and some carbon dioxide, and has less than half the energy density (i.e., BTU content) of natural gas. Syngas is combustible and is often used as a fuel source or as an intermediate for the production of other chemicals.
  • “Ton” or “ton” refers to U.S. short ton, i.e. about 907.2 kg (2000 lbs).
  • tar includes, without limitation, a gaseous tar, a liquid tar, a solid tar, a tar-forming substances, or mixtures thereof, which generally comprise hydrocarbons and derivatives thereof.
  • One large family of techniques includes analytical methods based on liquid or gas phase chromatography coupled with a detector. The most frequent detectors in the case of measurement of tars are the flame-ionization detector (FID) and the mass spectrometer.
  • FID flame-ionization detector
  • spectrometric methods which include detecting and analyzing a spectrum, This is for example infrared, ultraviolet (UV) or luminescence spectrometry, and LIBS (Laser- Induced Breakdown Spectroscopy) technique.
  • LIBS Laser- Induced Breakdown Spectroscopy
  • Another technique for monitoring of combustion gases is FTIR (Fourier Transform InfraRed) infrared spectrometry. Miscellaneous documents mention this technique, such as for example WO2006015660, WO03060480 and U.S. Pat. No. 5,984,998.
  • the amount of tar may be expressed as equivalent ppm of carbon.
  • the hydrocarbon may be benzene or an alcohol, such as methanol.
  • a tar concentration equivalent or tar equivalents most preferably corresponds to as equivalent ppm (molar) of benzene. The tar concentration is usefully measured at the outlet of the gasification apparatus and upstream of any substantial cooling of the syngas.
  • a gasification process for producing syngas includes gasifying carbonaceous material in a gasification apparatus to produce syngas that includes carbon monoxide (CO) and carbon dioxide (C0 2 ) and cooling said syngas in a syngas cooler or waste heat boiler and optionally further treating the cooled syngas with chemicals to remove contaminants and then further treating the chemical containing syngas in a dust collection system, e.g. a bag-house.
  • a gasification apparatus to produce syngas that includes carbon monoxide (CO) and carbon dioxide (C0 2 ) and cooling said syngas in a syngas cooler or waste heat boiler and optionally further treating the cooled syngas with chemicals to remove contaminants and then further treating the chemical containing syngas in a dust collection system, e.g. a bag-house.
  • CO carbon monoxide
  • C0 2 carbon dioxide
  • the process includes operating the gasification apparatus in a start-up mode with a reduced rate of feed, optionally with a high oxygen input per unit mass of carbonaceous material (e.g., stoichiometric or near stoichiometric or above stoichiometric amount of oxygen) to produce a first syngas with low CO content i.e. with low CO/CO2 ratio, e.g. CO/CO2 molar ratio less than about 0.5.
  • the process includes operating the gasification apparatus in a production mode, i.e.
  • CO/CO2 molar ratio in the second syngas is greater than about 1.0.
  • the process includes operating the gasification apparatus in a start-up mode until the gasification apparatus and equipment downstream of the gasification apparatus are adequately warmed up.
  • the process therefore, includes measuring temperatures of at one or more points (locations) inside and downstream of the gasification apparatus.
  • the process includes measuring temperatures of syngas (e.g. first syngas) at one or more points (locations) inside and downstream of the gasification apparatus.
  • operation of the gasification apparatus transitions from start-up mode to production mode after one or more points (locations) inside and downstream of the gasification apparatus attain target temperatures.
  • operation of the gasification apparatus transitions from start-up mode to production mode after temperature of syngas (first syngas) prior to entering syngas cooler attains a first target temperature.
  • operation of the gasification apparatus transitions from start-up mode to production mode after temperature of syngas (first syngas) at exit of dust-coUection system (e.g. bag-house) attains a second target temperature.
  • all or part of the first syngas produced during this start-up mode of operation can be passed through the syngas cooler to produce a cooled first syngas.
  • all or part of the first syngas produced during this start-up mode of operation can be sent to a thermal oxidation unit for processing and disposal.
  • all or a part of first syngas is sent to a thermal oxidation unit until temperature of first syngas at entry of said syngas cooler attains the first target temperature.
  • all or a part of first syngas is sent to a thermal oxidation unit during operation of gasification apparatus in start-up mode.
  • operation of the gasification apparatus transitions to production mode after the temperature of first syngas at syngas cooler entry attains a first target temperature. In one aspect, operation of the gasification apparatus transitions to production mode after the temperature of first syngas at exit of dust collection system (e.g. bag-house) attains a second target temperature. Addition of carbonaceous material and molecular oxygen into the gasification apparatus is continued, however, addition of molecular oxygen per unit mass of carbonaceous material in said gasification apparatus is reduced in order to produce a second syngas with high CO content or with high CO/C0 2 ratio, e.g. CO/CO 2 molar ratio greater than that of first syngas.
  • CO/CO 2 molar ratio in the second syngas is greater than about 1 .0.
  • All or part of the first syngas produced during this production mode of operation can be passed through the syngas cooler to produce a cooled second syngas.
  • all or part of the second syngas produced during this production mode of operation can be sent to a thermal oxidation unit for processing and disposal.
  • the process is effective for providing a CO/CO 2 molar ratio in said first syngas of less than about 0.5. In one aspect, the CO/CO2 molar ratio in said first syngas is less than about 0.25. In another aspect, the CO/CO 2 molar ratio in said first syngas is less than about 0.1. It is desirable to have more CO and less C0 2 in the second syngas. In one aspect, the process is effective for providing a CO/C0 2 molar ratio in said second syngas of greater than about 1.0. In one aspect, the CO/C0 2 molar ratio in said second syngas is greater than about 1.5.
  • a sub -stoichiometric amount of oxygen is supplied to the gasification apparatus in order to promote production of carbon monoxide during operation in production mode. Therefore, in one aspect, during operation in production mode, the ratio of amount of molecular oxygen input to total amount of molecular oxygen required to completely oxidize all carbon contained in carbonaceous material feed to carbon dioxide is in a range of 0.1 to 0.9, in one aspect 0.1 to 0.8, in another aspect 0.1 to 0.7, and in another aspect 0.1 to 0.45. In one aspect, during operation in start-up mode, the ratio of amount of molecular oxygen input to total amount of molecular oxygen required to completely oxidize all carbon contained in carbonaceous material feed to carbon dioxide is in a range of 0.5 to 2.0.
  • the ratio of amount of molecular oxygen input to total amount of molecular oxygen required to completely oxidize all carbon contained in carbonaceous material feed to carbon dioxide is in a range of 0.75 to 1.5. In one aspect, during operation in start-up mode, the ratio of amount of molecular oxygen input to total amount of molecular oxygen required to completely oxidize all carbon contained in carbonaceous material feed to carbon dioxide is in a range of 0.9 to 1.1.
  • the target temperatures are selected in a way that occurrence of fouling or deposit formation inside and downstream of the gasification apparatus can be avoided or reduced.
  • the first target temperature can be about 700°C to about 1000°C. In one aspect, the first target temperature can be about 750°C to about 850°C.
  • the second target temperature at an exit of the dust collection system can be about 100°C to about 200°C. In one aspect, the second target temperature can be about 100°C to about 150°C.
  • the reduction of the rate of addition of molecular oxygen per unit mass of carbonaceous material can be accomplished by increasing the rate of addition of carbonaceous material.
  • the rate of addition of carbonaceous material feed is kept significantly lower than that for production mode of operation while keeping the rate of addition of molecular oxygen at the same level as in each mode of operation.
  • the reduction of the rate of addition of molecular oxygen per unit mass of carbonaceous material can be accomplished by decreasing rate of addition of molecular oxygen.
  • the rate of addition of carbonaceous material feed is kept the same for start-up mode of operation and the production mode of operation but the rate of addition of molecular oxygen is decreased.
  • the rate of addition of molecular oxygen is decreased as the mode of operation is changed from start-up mode to production mode while rate of addition of carbonaceous material is increased.
  • Occurrence of fouling or deposit formation can be avoided or reduced in the syngas cooler by taking an additional measure of assuring a high enough linear velocity of gas flowing through the syngas cooler.
  • a linear velocity measured at the inlet of the syngas cooler is greater than about 15 meters/second, in another aspect, greater than about 20 meters/second, and in another aspect, about 24 meters/second is desirable.
  • the linear velocity measured at an inlet of the syngas cooler is between about 15 to about 30 meters/second, and in another aspect, about 22 to about 26 meters/second.
  • Increased linear velocity can be accomplished by increasing the volumetric flow rate of gas and/or decreasing the cross sectional area of flow.
  • the volumetric flow rate can be increased by recycling all or part of the gas exiting the syngas cooler back to the syngas cooler inlet.
  • an increased linear velocity is attained by mixing at least a portion of the cooled first syngas with at least a portion of first syngas prior to passing through said syngas cooler.
  • an increased linear velocity is attained by mixing at least a portion of cooled second syngas with at least a portion of second syngas prior to passing through said syngas cooler.
  • Increased volumetric flow rate can also be obtained by increasing the inert content of the gas.
  • the use of recycled cooled syngas enables optimum exchanger velocities to be maintained when the syngas production rate is reduced for whatever reason, including during start-up, shut-down and feedstock transitions.
  • an increased linear velocity is attained by using air as a molecular oxygen source especially during start-up mode of operation.
  • the gasification apparatus may include any gasification equipment described in prior art such as, but not limited to moving bed, fixed bed, fluidized bed, entrained flow, counter-current ("up draft"), co-current ("down draft"), counter-current fixed bed, co- current fixed bed, counter-current moving bed, co-current moving bed cross draft, hybrid, cross flow, cross flow moving bed, or a part thereof.
  • the gasification apparatus comprises a cross flow unit.
  • the gasification apparatus comprises a cross flow moving bed unit.
  • the gasification apparatus includes a gasification zone wherein carbonaceous material is contacted with oxygen containing gas at a relatively low temperature (e.g. below the ash fusion temperature) to produce a raw syngas and a heat treatment zone wherein the raw syngas undergoes heat treatment or conditioning in the presence of an additional amount of oxygen at a higher temperature (e.g. above the ash fusion temperature) to produce a hot syngas.
  • a relatively low temperature e.g. below the ash fusion temperature
  • a heat treatment zone wherein the raw syngas undergoes heat treatment or conditioning in the presence of an additional amount of oxygen at a higher temperature (e.g. above the ash fusion temperature) to produce a hot syngas.
  • pressure is atmospheric or greater than atmospheric.
  • air leakage may be allowed.
  • the gasification apparatus or the gasification zone includes multiple sections or gasification hearths for contacting said carbonaceous material with a first molecular oxygen-containing gas and optionally with one or more of steam and C0 2 to gasify a portion of said carbonaceous material and to produce a first gaseous product.
  • the gasification apparatus or gasification zone comprises 1 , 2, 3, 4, 5, 6, 7, 8, 9, or 10 sections or gasification hearths.
  • Gas inlets for introduction of molecular oxygen can be attached to the gasification apparatus or gasification zone or one or more hearths contained therein.
  • Steam or C0 2 may also be introduced through one or more of these gas inlets.
  • one or more of molecular oxygen, steam and C0 2 are pre-mixed prior to supplying to the gas inlets attached to the gasification apparatus or the gasification zone or to one or more hearths contained therein.
  • the heat treatment zone may accomplish one or more of cracking and partial oxidation of any tar contained in raw syngas.
  • the heat treatment zone can be a horizontal or a vertical chamber with circular or square or rectangular or any other cross section.
  • the heat treatment zone can be inclined to the horizontal or vertical direction.
  • the heat treatment zone is connected to the gasification zone through one or more connecting zones.
  • a gas inlet can be attached directly to the heat treatment zone.
  • One or more gas inlets can be attached to one or more connecting zones (throats).
  • Molecular oxygen containing gas can be introduced directly into the heat treatment zone.
  • Molecular oxygen containing gas can be introduced into the heat treatment zone through one or more gas inlets attached to one or more connecting zones.
  • Undesirable hot spots might be created in said gasification-apparatus or in the gasification zone or hearths contained therein due to uneven distribution of molecular oxygen containing gas in said carbonaceous material feed. This may produce poor quality syngas. Formation of hot spots can be reduced or prevented by injecting one or more of steam and carbon dioxide into one or more of said gasification apparatus.
  • carbonaceous material feed may be treated with steam along with molecular oxygen in the gasification apparatus.
  • Carbonaceous material feed may be treated with C0 2 gas along with molecular oxygen in the gasification apparatus.
  • co-feeding steam or C0 2 may not be advantageous.
  • Co-feeding steam or CO 2 may be advantageous and important during operation in production mode.
  • the source of molecular oxygen can be one or more of air, oxygen enriched air or pure oxygen.
  • the total amount of molecular oxygen introduced in the gasification apparatus during operation in production mode can be about 0 to about 75 lb-moles per ton of carbonaceous material on a dry basis, in another aspect about 0 to about 50 lb-moles per ton of carbonaceous material on a dry basis, and in another aspect about 40 to about 60 lb- moles per ton of carbonaceous material on a dry basis.
  • the total amount of molecular oxygen introduced in the gasification apparatus during operation in start-up mode can be in a range of about 0 to about 125 lb-moles per ton of carbonaceous material on a dry basis, in another aspect about 0 to about 100 lb-moles per ton of carbonaceous material on a dry basis, and in another aspect about 0 to about 50 lb-moles per ton of carbonaceous material on a dry basis.
  • the total amount of steam introduced in the gasification apparatus can be about 0 to about 50 lb-moles per ton of carbonaceous material feed on a dry basis.
  • the total amount of carbon dioxide gas introduced in the gasification apparatus can be about 0 to about 50 lb-moles per ton of carbonaceous material feed on a dry basis. In one aspect, both steam and carbon dioxide gas are introduced in the gasification apparatus.
  • the carbonaceous material fed to the gasifier may include carbonaceous material, carbonaceous liquid product, carbonaceous industrial liquid recycle, carbonaceous municipal solid waste (msw), carbonaceous urban waste, carbonaceous agricultural material, carbonaceous forestry material, carbonaceous wood waste, carbonaceous construction material, carbonaceous vegetative material, carbonaceous industrial waste, carbonaceous fermentation waste, carbonaceous petrochemical co-products, carbonaceous alcohol production co-products, carbonaceous coal, tires, plastics, waste plastic, coke oven tar, fibersoft, lignin, black liquor, polymers, waste polymers, polyethylene terephthalate (PETA), polystyrene (PS), sewage sludge, animal waste, crop residues, energy crops, forest processing residues, wood processing residues, livestock wastes, poultry wastes, food processing residues, fermentative process wastes, ethanol co-products, spent grain, spent microorganisms, or their combinations.
  • carbonaceous material carbonaceous liquid product
  • the carbonaceous material fed to the gasifier comprises a plurality of carbonaceous materials selected from carbonaceous material, carbonaceous liquid product, carbonaceous industrial liquid recycle, carbonaceous municipal solid waste (msw), carbonaceous urban waste, carbonaceous agricultural material, carbonaceous forestiy material, carbonaceous wood waste, carbonaceous construction material, carbonaceous vegetative material, carbonaceous industrial waste, carbonaceous fermentation waste, carbonaceous petrochemical co-products, carbonaceous alcohol production co-products, carbonaceous coal, tires, plastics, waste plastic, coke oven tar, fibersoft, lignin, black liquor, polymers, waste polymers, polyethylene terephthalate (PETA), polystyrene (PS), sewage sludge, animal waste, crop residues, energy crops, forest processing residues, wood processing residues, livestock wastes, poultry wastes, food processing residues, fermentative process wastes, ethanol co-products, spent grain, spent microorganisms, or their combinations.
  • carbonaceous materials
  • said carbonaceous material includes water. In one aspect, said carbonaceous material includes less than about 50 wt% water. In one aspect, said carbonaceous material includes less than about 25 wt% water. In one aspect, said carbonaceous material includes less than about 15 wt% water. In one aspect, the moisture content of said carbonaceous material is decreased by pre-drying. In one aspect, said carbonaceous material includes greater than about 25 wt% carbon on a dry or water free basis. In one aspect said carbonaceous material includes greater than about 50 wt% carbon on a dry or water free basis. In one aspect, said carbonaceous material includes about 0 to about 50 wt% oxygen on a dry or water free basis.
  • said carbonaceous material includes about 0 to about 25 wt% hydrogen on a dry or water free basis. In one aspect, said carbonaceous material includes less than about 25 wt% ash on a dry or water free basis. In one aspect said carbonaceous material includes less than about 15 wt% ash on a dry or water free basis.
  • syngas produced by the gasification apparatus can be cooled in a syngas cooler to produce a cooled syngas for downstream use, e.g. fermentation to produce chemicals such as acetic acid, ethanol, etc.
  • the syngas cooler may be heat exchange equipment or a heat exchanger known in the art.
  • a syngas cooler can be a selection from: shell-and-tube heat exchanger, plate heat exchanger, plate-and- frame heat exchanger, tubular heat exchanger, double-pipe heat exchanger, hair-pin heat exchanger, single-pass heat exchanger, multi-pass heat exchanger, plate-fin heat exchanger, spiral heat exchanger, and combinations thereof.
  • Cooled syngas may contain contaminants that should be removed prior to downstream use. Removal of contaminants can be accomplished by treating cooled syngas with chemical agents. Thus, one or more chemical agents may be added to cooled syngas to produce a chemical containing cooled syngas.
  • the chemical containing cooled syngas may be processed in a dust collection system (e.g. a bag-house) to remove chemical residues to thus produce a clean cooled syngas. Clean cooled syngas may be sent to a down stream processing or to a thermal oxidation unit. The clean cooled syngas can be optionally further cooled in a quench tower prior to downstream use.
  • the dust collection system is effective for capturing, separation or filtering of solid particles (fine particles, dust) from the gas.
  • the dust collection system may include one or more of a blower, a dust filter, a filter-cleaning system, and a dust receptacle or dust removal system.
  • the dust collection system can be an inertial separator type dust collector, a fabric filter type dust collector (bag-house), a wet scrubber, an electrostatic precipitator, or a unit collector.
  • the dust collection system is a bag-house.
  • the heat treatment zone may be cold during start-up and may be prone to fouling or deposit formation or may contribute to fouling or deposit formation in the downstream piping or syngas cooler. It is, therefore, often preferred that the gasification apparatus is operated in start-up mode until the heat treatment zone is adequately warmed up.
  • the gasification apparatus is operated in start-up mode until the heat treatment zone attains a temperature of about 900°C. Operation in production mode is not started until the heat treatment zone attains at least about 900°C temperature.
  • all or part of the first syngas produced is sent to a thermal oxidation unit until the heat treatment zone attains at least about 900°C temperature.
  • the gasification apparatus is operated in a start-up mode until the heat treatment zone attains a temperature of about 1000°C. Operation in production mode is not started until the heat treatment zone attains at least about 1000°C.
  • all or part of the first syngas produced is sent to a thermal oxidation unit until the heat treatment zone attains at least about 1000°C.
  • At least a portion of syngas exiting the syngas cooler is recycled back to the gasification apparatus in order to cool the syngas cooler inlet temperature and/or increase the linear velocity of gas entering syngas cooler. In one aspect, at least a portion of syngas exiting the syngas cooler is recycled back to the connecting zone of a gasification apparatus in order to increase the linear velocity of gas entering syngas cooler as well as through the connecting zone wherein the gasification zone includes a gasification zone and a heat treatment zone connected by a connecting zone.
  • Figures 1 to 4 illustrates various aspects of the process.
  • Figure 1 is a schematic diagram of one aspect of a process comprising gasification of carbonaceous material by treating with molecular oxygen in a gasification apparatus to produce a hot syngas and subsequent cooling of said hot syngas in a syngas cooler to produce a cooled syngas.
  • a carbonaceous material feed (100) is introduced in the gasification-apparatus (200).
  • a molecular oxygen containing gas (150) is supplied to the gasification apparatus and thus the carbonaceous material feed is treated with molecular oxygen in order to initiate and facilitate chemical transformation of carbonaceous material.
  • At least a portion of the carbonaceous material feed is gasified in the gasification apparatus to produce a gaseous product or syngas (250).
  • Supply of oxygen into the gasification-apparatus can be controlled in order to control relative amounts of carbon monoxide (CO) and carbon dioxide (C0 2 ) produced from gasification of the carbonaceous material.
  • Hot syngas is subsequently cooled in a syngas cooler (300) to produce a cooled syngas (350).
  • a stream of ash (220) is removed from the gasification apparatus.
  • FIG. 2 is a schematic diagram of an aspect of a process including gasification of carbonaceous material by treating with molecular oxygen in a gasification apparatus to produce a hot syngas and subsequent cooling of said hot syngas in a syngas cooler to produce a cooled syngas; wherein at least a part of said cooled syngas is recycled and mixed with said hot syngas prior to entry into syngas cooler.
  • a carbonaceous material feed (100) is introduced in the gasification-apparatus (200).
  • a molecular oxygen containing gas (150) is supplied to the gasification apparatus and thus the carbonaceous material feed is treated with molecular oxygen in order to initiate and facilitate chemical transformation of carbonaceous material.
  • At least a portion of the carbonaceous material feed is gasified in the gasification apparatus to produce a gaseous product or syngas (250).
  • Supply of oxygen into the gasification-apparatus can be controlled in order to control relative amounts of carbon monoxide (CO) and carbon dioxide (C0 2 ) produced from gasification of the carbonaceous material.
  • Hot syngas is subsequently cooled in a syngas cooler (300) to produce a cooled syngas (350). At least a part of said cooled syngas (450) is recycled and mixed with said hot syngas prior to entry into syngas cooler.
  • a compressor (400) is used to facilitate recycle of cooled syngas.
  • a stream of ash (220) is removed from the gasification apparatus.
  • Figure 3 is a schematic diagram of an aspect of a process that includes gasification of carbonaceous material by treating with molecular oxygen in a gasification apparatus to produce a hot syngas and subsequent cooling of said hot syngas in a syngas cooler to produce a cooled syngas; wherein at least a part of said cooled syngas is recycled and mixed with said hot syngas prior to entry into syngas cooler; and wherein the gasification apparatus comprises two reaction zones, e.g., a gasification zone and a heat treatment zone connected through a connecting zone.
  • a carbonaceous material feed ( 00) is introduced in the gasification zone (201) of said gasification-apparatus.
  • a molecular oxygen containing gas (150) is supplied to the gasification zone of said gasification apparatus and thus the carbonaceous material feed is treated with molecular oxygen in order to initiate and facilitate chemical transformation of carbonaceous material.
  • At least a portion of the carbonaceous material feed is gasified in the gasification zone to produce a raw gaseous product (raw syngas).
  • the raw syngas passes through the connecting zone (203).
  • Molecular oxygen (202) is introduced in the connecting zone to be mixed with said raw syngas.
  • Mixture comprising raw syngas and molecular oxygen enters the heat treatment zone (204).
  • Molecular oxygen can also be introduced in the heat treatment zone.
  • Raw syngas undergoes heat treatment in the heat treatment zone to produce a hot syngas (250).
  • Supply of oxygen into the gasification-apparatus can be controlled in order to control relative amounts of carbon monoxide (CO) and carbon dioxide (C0 2 ) produced from gasification of the carbonaceous material.
  • Plot syngas is subsequently cooled in a syngas cooler (300) to produce a cooled syngas (350). At least a part of said cooled syngas (450) is recycled and mixed with said hot syngas prior to entry into syngas cooler.
  • a compressor (400) is used to facilitate recycle of cooled syngas.
  • a stream of ash (220) is removed from the gasification apparatus.
  • Figure 4 is a schematic diagram of a process that includes gasification of carbonaceous material by treating with molecular oxygen in a gasification apparatus to produce a hot syngas and subsequent cooling of said hot syngas in a syngas cooler to produce a cooled syngas; wherein at least a part of said cooled syngas is recycled and mixed with said hot syngas prior to entry into syngas cooler; wherein at least a portion of one or more of hot and cooled syngas can be sent to a thermal oxidation unit; and wherein at least a portion of said cooled syngas can be processed in a bag-house.
  • a carbonaceous material feed (100) is introduced in the gasification-apparatus (200).
  • a molecular oxygen containing gas (150) is supplied to the gasification apparatus and thus the carbonaceous material feed is treated with molecular oxygen in order to initiate and facilitate chemical transformation of carbonaceous material.
  • At least a portion of the carbonaceous material feed is gasified in the gasification apparatus to produce a gaseous product or syngas (250).
  • Supply of oxygen into the gasification-apparatus can be controlled in order to control relative amounts of carbon monoxide (CO) and carbon dioxide (C0 2 ) produced from gasification of the carbonaceous material.
  • Hot syngas is subsequently cooled in a syngas cooler (300) to produce a cooled syngas (350). At least a part of said cooled syngas (450) is recycled and mixed with said hot syngas prior to entry into syngas cooler.
  • a compressor (400) is used to facilitate recycle of cooled syngas. At least a portion of hot syngas can be sent to a thermal oxidation unit (700) for processing and disposal (750). At least portion of cooled syngas can be sent to a thermal oxidation unit. Cooled syngas may contain contaminants that should be removed prior to downstream use. Removal of contaminants can be accomplished by adding chemical agents. Thus one or more chemical agents (500) can be added to cooled syngas to produce a chemical containing cooled syngas (550), The chemical containing cooled syngas is processed in a bag-house (600) to remove chemical residues (chemical agents with contaminants) and to produce a clean cooled syngas (650) that is either sent to down stream processing or to thermal oxidation unit. The clean cooled syngas can be optionally further cooled in a quench tower prior to downstream use (not shown on diagram). A stream of ash (220) is removed from the gasification apparatus.
  • Example 1 Solid Load of Syngas Produced by Gasification in Production Mode
  • the gasification apparatus was operated in a start-up mode by providing carbonaceous materials to the gasifier at a feed rate of about half as much as that used in a production mode.
  • Oxygen was supplied to the gasifier at a feed rate of about 40 to 50 lb- mole ton of carbonaceous material on a dry basis. As described previously, some air leakage into the gasifier was allowed that increase oxygen availability.
  • a carbonaceous material feed rate was increased into the gasification apparatus.
  • a molecular oxygen containing gas was supplied to the gasification apparatus at the rate of about 50 to about 90 lb-moles per ton of water-free carbonaceous material.
  • the gasifier was also fed a stream of carbon dioxide at the rate of about 10 to about 1 lb-moles per ton of water- free carbonaceous material.
  • Hot syngas is produced during this operation is subsequently cooled in a syngas cooler to produce a cooled syngas.
  • Cooled syngas is processed in a bag-house to remove solid residues and to produce a clean cooled syngas.
  • the clean cooled syngas comprised CO in the range of about 25 to about 35 mole%, C0 2 in the range of about 30 to about 40 mole%, I3 ⁇ 4 in the range of about 10 to about 20 mole%, N 2 in the range of about 15 to about 25 mole% and small amount of CH 4 .
  • the bag-house removed about 1.5 to about 3.5 lbs solid per hour per 1000 lbs per hour clean cooled syngas produced.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Sustainable Energy (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Industrial Gases (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Treatment Of Sludge (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un procédé de production de gaz de synthèse qui est reconnu être efficace dans des procédés en aval. Le procédé de fabrication du gaz de synthèse consiste à faire fonctionner un appareil de gazéification dans un mode de démarrage jusqu'à ce que l'appareil de gazéification et l'équipement en aval de l'appareil de gazéification soient suffisamment réchauffés à une première température cible. Lorsqu'une première température cible est atteinte, le procédé est ensuite amené à fonctionner dans un mode de production afin de produire un second gaz de synthèse avec un rapport molaire CO/CO2 supérieur. Le fonctionnement dans un mode de démarrage jusqu'à ce qu'une première température cible soit atteinte fournit un procédé qui est efficace pour réduire l'encrassement dans un équipement en aval et pour fournir un second gaz de synthèse qui peut être refroidi et nettoyé de façon plus efficace.
PCT/US2012/032168 2011-04-06 2012-04-04 Processus de fonctionnement de procédé de production de gaz de synthèse à partir de matière carbonée WO2013032537A1 (fr)

Priority Applications (14)

Application Number Priority Date Filing Date Title
CN201280024944.1A CN103874750B (zh) 2011-04-06 2012-04-04 从含碳材料生产合成气的过程的运行方法
JP2014503951A JP6127323B2 (ja) 2011-04-06 2012-04-04 炭素質材料からシンガスを生成するためのプロセスの操作方法
EP12715788.1A EP2694624B1 (fr) 2011-04-06 2012-04-04 Processus de fonctionnement de procédé de production de gaz de synthèse à partir de matière carbonée
EA201370217A EA029848B1 (ru) 2011-04-06 2012-04-04 Способ осуществления процесса получения синтез-газа из углеродсодержащего материала
BR112013025718A BR112013025718B1 (pt) 2011-04-06 2012-04-04 processos para produzir e resfriar gás de síntese
MX2013011708A MX2013011708A (es) 2011-04-06 2012-04-04 Metodo de operacion de proceso para producir gas de sintesis a partir de material carbonico.
EP18203543.6A EP3453747A1 (fr) 2011-04-06 2012-04-04 Procédé de production de gaz de synthèse à partir de matière carbonée
AU2012302236A AU2012302236B2 (en) 2011-04-06 2012-04-04 Method of operation of process to produce syngas from carbonaceous material
CA2832431A CA2832431C (fr) 2011-04-06 2012-04-04 Processus de fonctionnement de procede de production de gaz de synthese a partir de matiere carbonee
KR1020137029101A KR101882544B1 (ko) 2011-04-06 2012-04-04 탄소질 재료로부터 합성가스를 생성하는 프로세스의 작동 방법
ES12715788T ES2708221T3 (es) 2011-04-06 2012-04-04 Procedimiento de operación de un proceso para producir sintegás a partir de material carbonoso
PL12715788T PL2694624T3 (pl) 2011-04-06 2012-04-04 Sposób działania sposobu wytwarzania gazu syntezowego z materiału węglowego
NZ617115A NZ617115B2 (en) 2011-04-06 2012-04-04 Method of operation of process to produce syngas from carbonaceous material
ZA2013/08269A ZA201308269B (en) 2011-04-06 2013-11-05 Method of operating of process to produce syngas from carbonaceous material

Applications Claiming Priority (8)

Application Number Priority Date Filing Date Title
US201161516646P 2011-04-06 2011-04-06
US201161516667P 2011-04-06 2011-04-06
US201161516704P 2011-04-06 2011-04-06
US61/516,646 2011-04-06
US61/516,704 2011-04-06
US61/516,667 2011-04-06
US13/427,247 US20120256131A1 (en) 2011-04-06 2012-03-22 Method of Operation of Process to Produce Syngas from Carbonaceous Material
US13/427,247 2012-03-22

Publications (1)

Publication Number Publication Date
WO2013032537A1 true WO2013032537A1 (fr) 2013-03-07

Family

ID=46965027

Family Applications (5)

Application Number Title Priority Date Filing Date
PCT/US2012/032006 WO2013147918A2 (fr) 2011-04-06 2012-04-03 Appareil et procédé pour la gazéification de substances carbonées pour produire un gaz de synthèse
PCT/US2012/032180 WO2012138766A2 (fr) 2011-04-06 2012-04-04 Système de génération de puissance à partir de procédé de fermentation de gaz de synthèse
PCT/US2012/032168 WO2013032537A1 (fr) 2011-04-06 2012-04-04 Processus de fonctionnement de procédé de production de gaz de synthèse à partir de matière carbonée
PCT/US2012/032160 WO2012138751A1 (fr) 2011-04-06 2012-04-04 Appareil et procédé pour l'élimination de goudron d'un gaz de synthèse
PCT/US2012/032174 WO2012138762A1 (fr) 2011-04-06 2012-04-04 Système refroidisseur de gaz de synthèse et son procédé de fonctionnement

Family Applications Before (2)

Application Number Title Priority Date Filing Date
PCT/US2012/032006 WO2013147918A2 (fr) 2011-04-06 2012-04-03 Appareil et procédé pour la gazéification de substances carbonées pour produire un gaz de synthèse
PCT/US2012/032180 WO2012138766A2 (fr) 2011-04-06 2012-04-04 Système de génération de puissance à partir de procédé de fermentation de gaz de synthèse

Family Applications After (2)

Application Number Title Priority Date Filing Date
PCT/US2012/032160 WO2012138751A1 (fr) 2011-04-06 2012-04-04 Appareil et procédé pour l'élimination de goudron d'un gaz de synthèse
PCT/US2012/032174 WO2012138762A1 (fr) 2011-04-06 2012-04-04 Système refroidisseur de gaz de synthèse et son procédé de fonctionnement

Country Status (20)

Country Link
US (9) US20120255301A1 (fr)
EP (9) EP3381997B1 (fr)
JP (6) JP6415320B2 (fr)
KR (6) KR101959581B1 (fr)
CN (8) CN105907423A (fr)
AR (4) AR085932A1 (fr)
AU (4) AU2012375190B2 (fr)
BR (5) BR112013025720B1 (fr)
CA (5) CA2832554C (fr)
CR (4) CR20130576A (fr)
EA (4) EA027557B1 (fr)
ES (5) ES2686289T3 (fr)
MX (4) MX2013011570A (fr)
MY (5) MY166661A (fr)
NZ (1) NZ710264A (fr)
PL (5) PL2694432T3 (fr)
RU (1) RU2603663C2 (fr)
TW (5) TWI541337B (fr)
WO (5) WO2013147918A2 (fr)
ZA (5) ZA201308271B (fr)

Families Citing this family (40)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010141629A1 (fr) 2009-06-02 2010-12-09 Thermochem Recovery International, Inc. Gazéifieur comprenant un système de génération d'énergie par pile à combustible intégré
WO2012061742A1 (fr) 2010-11-05 2012-05-10 ThermoChem Recovery International Système de circulation de solides et méthode de capture et de conversion de solides réactifs
US20120255301A1 (en) 2011-04-06 2012-10-11 Bell Peter S System for generating power from a syngas fermentation process
US9291390B2 (en) * 2011-05-11 2016-03-22 Shell Oil Company Process for producing purified synthesis gas
US8673181B2 (en) * 2011-08-11 2014-03-18 Kellogg Brown & Root Llc Systems and methods for starting up a gasifier
CN105584991B (zh) 2011-09-27 2019-05-14 国际热化学恢复股份有限公司 合成气净化系统和方法
WO2013142945A1 (fr) * 2012-03-29 2013-10-03 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources Brûleur supplémentaire pour la conversion de biomasse et d'un autre combustible associé
JP6248495B2 (ja) * 2013-09-18 2017-12-20 株式会社Ihi ガス化ガス中のタールの改質装置
US9631151B2 (en) * 2014-09-04 2017-04-25 Ag Energy Solutions, Inc. Apparatuses, systems, tar crackers, and methods for gasifying having at least two modes of operation
FI126357B (en) 2014-11-14 2016-10-31 Teknologian Tutkimuskeskus Vtt Oy Process and apparatus for gasification of raw material and gaseous product
US10774267B2 (en) * 2014-11-21 2020-09-15 Kevin Phan Method and device for converting municipal waste into energy
CN104845677A (zh) * 2015-03-30 2015-08-19 天津渤化永利化工股份有限公司 一种降低煤气化炉过热段入口合成气温度的方法
GB2539447B (en) 2015-06-16 2017-07-05 Sage & Time Llp Converting a carbonaceous feedstock into a product gas e.g. methane gas
WO2017115789A1 (fr) 2015-12-28 2017-07-06 国立研究開発法人理化学研究所 Composition pour récupérer ou améliorer la dégradation de fonctions physiologiques due au vieillissement
MX2018009906A (es) 2016-02-16 2018-09-07 Thermochem Recovery Int Inc Sistema y metodo de generacion de gas producto de energia integrada de dos etapas.
EP3210939A1 (fr) * 2016-02-24 2017-08-30 Casale SA Réacteur d'oxydation d'ammoniac dans la production d'acide nitrique
WO2017164888A1 (fr) 2016-03-25 2017-09-28 Thermochem Recovery International, Inc. Système et procédé de génération de produit gazeux intégré en énergie à trois étapes
ES2966552T3 (es) * 2016-06-03 2024-04-22 Wildfire Energy Pty Ltd Producción de un gas y métodos para ello
US10197015B2 (en) 2016-08-30 2019-02-05 Thermochem Recovery International, Inc. Feedstock delivery system having carbonaceous feedstock splitter and gas mixing
US10364398B2 (en) 2016-08-30 2019-07-30 Thermochem Recovery International, Inc. Method of producing product gas from multiple carbonaceous feedstock streams mixed with a reduced-pressure mixing gas
US10197014B2 (en) 2016-08-30 2019-02-05 Thermochem Recovery International, Inc. Feed zone delivery system having carbonaceous feedstock density reduction and gas mixing
JP6822025B2 (ja) * 2016-09-12 2021-01-27 株式会社Ihi タール改質装置
US11203725B2 (en) * 2017-04-06 2021-12-21 LLT International (Ireland) Ltd. Systems and methods for gasification of carbonaceous materials
US10329506B2 (en) 2017-04-10 2019-06-25 Thermochem Recovery International, Inc. Gas-solids separation system having a partitioned solids transfer conduit
US10717102B2 (en) 2017-05-31 2020-07-21 Thermochem Recovery International, Inc. Pressure-based method and system for measuring the density and height of a fluidized bed
US9920926B1 (en) 2017-07-10 2018-03-20 Thermochem Recovery International, Inc. Pulse combustion heat exchanger system and method
GB2567229A (en) * 2017-10-07 2019-04-10 Narasimhamurthy Prakashkumar Set-up for continuous production of H2 , CO, granulated fertiliser slag from the molten slag and sequestering CO2 from the flue exhaust
EP3694956B1 (fr) * 2017-10-12 2023-07-12 Danmarks Tekniske Universitet Unité de gazéification, procédé de production d'un gaz de produit et utilisation d'un tel procédé
US10099200B1 (en) 2017-10-24 2018-10-16 Thermochem Recovery International, Inc. Liquid fuel production system having parallel product gas generation
US11104877B2 (en) 2018-05-21 2021-08-31 Jupeng Bio, Inc. Composition for obtaining protein-rich nutrient supplements from bacterial fermentation process
JP7280951B2 (ja) * 2018-11-19 2023-05-24 ランザテク，インコーポレイテッド 発酵とガス化との統合
CN109652127A (zh) * 2018-11-30 2019-04-19 浙江天禄环境科技有限公司 一种利用低阶煤中挥发分制备包含c1-c2的烃类的方法和系统
US11447576B2 (en) 2019-02-04 2022-09-20 Eastman Chemical Company Cellulose ester compositions derived from recycled plastic content syngas
US11286436B2 (en) 2019-02-04 2022-03-29 Eastman Chemical Company Feed location for gasification of plastics and solid fossil fuels
WO2021032770A1 (fr) * 2019-08-21 2021-02-25 Ags Energy (Ireland) Limited Appareil et procédé de gazéification
US11555157B2 (en) 2020-03-10 2023-01-17 Thermochem Recovery International, Inc. System and method for liquid fuel production from carbonaceous materials using recycled conditioned syngas
GB2593231B (en) 2020-03-17 2022-03-23 Velocys Tech Limited Process
US11466223B2 (en) 2020-09-04 2022-10-11 Thermochem Recovery International, Inc. Two-stage syngas production with separate char and product gas inputs into the second stage
US11827859B1 (en) 2022-05-03 2023-11-28 NuPhY, Inc. Biomass gasifier system with rotating distribution manifold
WO2024107792A1 (fr) * 2022-11-16 2024-05-23 Sungas Renewables, Inc. Flexibilité de traitement accrue dans la gazéification

Citations (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4805561A (en) * 1987-12-11 1989-02-21 Shell Oil Company Coal gasification process with inhibition of quench zone plugging
EP0416242A1 (fr) * 1989-09-07 1991-03-13 Krupp Koppers GmbH Installation pour la production d'un gaz à partir de solides carbonifères finement divisés
DE4035293C1 (fr) * 1990-11-07 1992-01-02 Metallgesellschaft Ag, 6000 Frankfurt, De
WO1993018341A1 (fr) 1992-03-05 1993-09-16 Technische Universiteit Delft Procede et appareil de combustion d'un materiau carbone
US5984998A (en) 1997-11-14 1999-11-16 American Iron And Steel Institute Method and apparatus for off-gas composition sensing
US6033447A (en) * 1997-06-25 2000-03-07 Eastman Chemical Company Start-up process for a gasification reactor
US6435139B1 (en) 2000-12-14 2002-08-20 Borsig Gmbh Waste heat boiler for cooling hot syngas
WO2003060480A1 (fr) 2002-01-17 2003-07-24 L'air Liquide - Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de surveillance en temps reel de gaz de carneau de fours
WO2006015660A1 (fr) 2004-08-12 2006-02-16 Sms Demag Ag Mesure sans contact des fumees par spectroscopie irtf sur des unites metallurgiques
US7552701B2 (en) 2006-05-16 2009-06-30 Shell Oil Company Boiler for making super heated steam and its use
US7587995B2 (en) 2005-11-03 2009-09-15 Babcock & Wilcox Power Generation Group, Inc. Radiant syngas cooler
WO2009154788A2 (fr) 2008-06-20 2009-12-23 Ineos Usa Llc Procédés de séquestration de dioxyde de carbone dans des alcools par gazéification et fermentation
US20100044643A1 (en) * 2008-08-22 2010-02-25 Hunton Energy Holdings, LLC Low NOx Gasification Startup System
US20100090166A1 (en) * 2008-10-08 2010-04-15 Fournier Guillaume Guy Michel Process to prepare a gas mixture of hydrogen and carbon monoxide
US20100180503A1 (en) * 2008-01-29 2010-07-22 Mitsubishi Heavy Industries Ltd Starting method of coal gasifier and starting device therefor

Family Cites Families (106)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2815007A (en) * 1951-12-12 1957-12-03 Babcock & Wilcox Co Synthesis gas generator
US3787192A (en) * 1972-03-02 1974-01-22 Mcdowell Wellman Eng Co Process for coal gasification
NL178134C (nl) * 1974-06-17 1986-02-03 Shell Int Research Werkwijze en inrichting voor het behandelen van een heet produktgas.
US3963457A (en) * 1974-11-08 1976-06-15 Koppers Company, Inc. Coal gasification process
US3980592A (en) 1974-12-23 1976-09-14 Texaco Development Corporation Recovery of particulate carbon from synthesis gas
US4072625A (en) 1975-03-03 1978-02-07 Imperial Chemical Industries Limited Steam-hydrocarbon process
US4017271A (en) 1975-06-19 1977-04-12 Rockwell International Corporation Process for production of synthesis gas
US4172425A (en) * 1977-10-31 1979-10-30 Consumat Systems, Inc. Incinerator with improved means for transferring burning waste through the combustion chamber
DE2836175A1 (de) * 1978-08-18 1980-02-28 Metallgesellschaft Ag Verfahren zum vergasen fester, feinkoerniger brennstoffe
US4270493A (en) * 1979-01-08 1981-06-02 Combustion Engineering, Inc. Steam generating heat exchanger
US4326856A (en) * 1979-05-30 1982-04-27 Texaco Development Corporation Production of cleaned and cooled synthesis gas
US4279622A (en) * 1979-07-13 1981-07-21 Texaco Inc. Gas-gas quench cooling and solids separation process
US4248604A (en) * 1979-07-13 1981-02-03 Texaco Inc. Gasification process
US4308034A (en) * 1980-05-19 1981-12-29 Hoang Dinh C Apparatus for incinerating and gasifying biomass material
US4490156A (en) * 1981-06-10 1984-12-25 Texaco Inc. Partial oxidation system
IN156182B (fr) * 1981-11-16 1985-06-01 Shell Int Research
US4461674A (en) * 1981-12-31 1984-07-24 Allis-Chalmers Corporation Apparatus for recovery of different weight fractions of oil from shale
US4497637A (en) * 1982-11-22 1985-02-05 Georgia Tech Research Institute Thermochemical conversion of biomass to syngas via an entrained pyrolysis/gasification process
JPS61250092A (ja) * 1985-04-30 1986-11-07 Ishikawajima Harima Heavy Ind Co Ltd 固体有機物のガス化方法
US4749383A (en) * 1986-06-04 1988-06-07 Mansfield Carbon Products Method for producing low and medium BTU gas from coal
US4805562A (en) * 1987-12-11 1989-02-21 Shell Oil Company Coal gasification process with inhibition of quench zone plugging
US4823742A (en) * 1987-12-11 1989-04-25 Shell Oil Company Coal gasification process with inhibition of quench zone plugging
US4823741A (en) 1987-12-11 1989-04-25 Shell Oil Company Coal gasification process with inhibition of quench zone plugging
US4865625A (en) * 1988-05-02 1989-09-12 Battelle Memorial Institute Method of producing pyrolysis gases from carbon-containing materials
DE3816340A1 (de) * 1988-05-13 1989-11-23 Krupp Koppers Gmbh Verfahren und vorrichtung zum kuehlen eines heissen produktgases, das klebrige bzw. schmelzfluessige partikel enthaelt
US4859213A (en) * 1988-06-20 1989-08-22 Shell Oil Company Interchangeable quench gas injection ring
DK315289A (da) * 1988-06-30 1989-12-31 Shell Int Research Fremgangsmaade til omdannelse af forureninger i en raa hoejtrykssyntesegasstroem med hoej temperatur
JPH0816229B2 (ja) * 1988-10-18 1996-02-21 三菱重工業株式会社 ガス中のタールおよびアンモニアの分解装置
US4959080A (en) * 1989-06-29 1990-09-25 Shell Oil Company Process for gasification of coal utilizing reactor protected interally with slag coalescing materials
DE4310447A1 (de) * 1993-03-31 1994-10-06 Krupp Koppers Gmbh Verfahren zur Kühlung von durch Vergasung gewonnenem Rohgas
JP2544584B2 (ja) * 1994-04-11 1996-10-16 株式会社日立製作所 石炭ガス化炉及び石炭ガス化炉の使用方法
ZA969708B (en) * 1995-12-15 1997-06-20 Krupp Polysius Ag Prevention of snowmen and removal of lumps in clinker coolers
RU2117687C1 (ru) * 1996-12-20 1998-08-20 Акционерное общество открытого типа "Энергетический институт им.Г.М.Кржижановского" Установка для термической переработки твердых топлив
US5944034A (en) * 1997-03-13 1999-08-31 Mcnick Recycling, Inc. Apparatus and method for recycling oil laden waste materials
JP4137266B2 (ja) * 1999-01-28 2008-08-20 新日本製鐵株式会社 還元鉄製造方法
DE19949142C1 (de) * 1999-10-12 2001-05-10 Thermoselect Ag Vaduz Verfahren und Vorrichtung zur Entsorgung und Nutzbarmachung von Abfallgütern
US7090707B1 (en) * 1999-11-02 2006-08-15 Barot Devendra T Combustion chamber design for a quench gasifier
BR0112251B1 (pt) 2000-07-25 2013-04-09 mÉtodos contÍnuos para produÇço de etanol a partir da fermentaÇço bacteriana anaeràbica de um substrato gasoso.
US20030046868A1 (en) * 2001-03-12 2003-03-13 Lewis Frederic Michael Generation of an ultra-superheated steam composition and gasification therewith
JP2003161414A (ja) * 2001-11-27 2003-06-06 Mitsubishi Heavy Ind Ltd ストーカ式廃棄物ガス化焼却装置及び焼却方法
JP3824267B2 (ja) * 2002-11-20 2006-09-20 日本碍子株式会社 廃棄物からの可燃性ガス回収装置
JP4255279B2 (ja) * 2002-12-27 2009-04-15 独立行政法人科学技術振興機構 固体燃料ガス化システム
JP2005060533A (ja) * 2003-08-12 2005-03-10 Chugai Ro Co Ltd バイオマスガス化システムの燃料ガス改質装置
US20050095183A1 (en) * 2003-11-05 2005-05-05 Biomass Energy Solutions, Inc. Process and apparatus for biomass gasification
EP1531147A1 (fr) * 2003-11-06 2005-05-18 CASALE ChEMICALS S.A. Procédé de reformage secondaire catalytique et réacteur permettant de mettre en oeuvre ledit procédé
JP4312632B2 (ja) * 2004-03-03 2009-08-12 中外炉工業株式会社 バイオマスガス化システムおよびその運転方法
KR100637340B1 (ko) * 2004-04-09 2006-10-23 김현영 고온 개질기
JP2006028211A (ja) * 2004-07-12 2006-02-02 Kawasaki Heavy Ind Ltd 廃棄物ガス化装置
JP2006131820A (ja) * 2004-11-09 2006-05-25 Ishikawajima Harima Heavy Ind Co Ltd 流動層ガス化方法及び装置
FI20055237L (fi) 2005-05-18 2006-11-19 Foster Wheeler Energia Oy Menetelmä ja laitteisto hiilipitoisen materiaalin kaasuttamiseksi
CN100543116C (zh) * 2005-08-19 2009-09-23 中国科学院过程工程研究所 制备无焦油产品气的贫氧流化燃烧下吸式气化方法及装置
MY148126A (en) * 2005-10-21 2013-02-28 Taylor Biomass Energy Llc Process and system for gasification with in-situ tar removal
JP4790412B2 (ja) 2005-12-28 2011-10-12 中外炉工業株式会社 バイオマスガス化装置
CA2647267C (fr) 2006-03-24 2015-03-03 Silvagas Corporation Systeme de gazeification de biomasse
NZ546496A (en) 2006-04-07 2008-09-26 Lanzatech New Zealand Ltd Gas treatment process
FI118647B (fi) * 2006-04-10 2008-01-31 Valtion Teknillinen Menetelmä tervamaisia epäpuhtauksia sisältävän kaasun reformoimiseksi
US7857995B2 (en) * 2006-04-11 2010-12-28 Thermo Technologies, Llc Methods and apparatus for solid carbonaceous materials synthesis gas generation
MX2008014200A (es) * 2006-05-05 2009-06-04 Plasco Energy Ip Holdings S L Gasificador orientado horizontalmente con sistema de transferencia lateral.
NZ573217A (en) 2006-05-05 2011-11-25 Plascoenergy Ip Holdings S L Bilbao Schaffhausen Branch A facility for conversion of carbonaceous feedstock into a reformulated syngas containing CO and H2
JP2009536262A (ja) 2006-05-05 2009-10-08 プラスコエナジー アイピー ホールディングス、エス．エル．、ビルバオ、シャフハウゼン ブランチ ガスコンディショニングシステム
KR20090040406A (ko) * 2006-05-05 2009-04-24 플라스코에너지 아이피 홀딩스, 에스.엘., 빌바오, 샤프하우젠 브랜치 플라즈마 토치 가열을 사용하는 가스 재구성 시스템
US20080169449A1 (en) 2006-09-08 2008-07-17 Eltron Research Inc. Catalytic membrane reactor and method for production of synthesis gas
US8444725B2 (en) 2006-09-11 2013-05-21 Purdue Research Foundation System and process for producing synthetic liquid hydrocarbon
CN1931959B (zh) * 2006-09-28 2010-10-20 武汉凯迪工程技术研究总院有限公司 利用生物质制造合成气的复合循环式高温气化工艺方法
EP1918352B1 (fr) 2006-11-01 2009-12-09 Shell Internationale Researchmaatschappij B.V. Alimentation carbonée solide pour procédé liquide
AU2008215182B2 (en) 2007-02-16 2011-09-22 Corky's Carbon And Combustion Pty Ltd Drying and gasification process
WO2008104058A1 (fr) * 2007-02-27 2008-09-04 Plasco Energy Group Inc. Système de gazéification avec conversion de charge d'alimentation/produit de carbonisation traité et reformulation de gaz
CN101285004B (zh) * 2007-04-11 2010-12-15 中国科学院工程热物理研究所 一种多功能能源装置
CN101410482A (zh) * 2007-04-18 2009-04-15 片山优久雄 焦炉煤气用改性器
US20080280236A1 (en) 2007-05-08 2008-11-13 Wright Roger G Solid fuel compositions, processes for preparing solid fuel, and combustion processes
US20090014689A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing syngas and alcohols
US8153027B2 (en) 2007-07-09 2012-04-10 Range Fuels, Inc. Methods for producing syngas
BRPI0812629A2 (pt) * 2007-07-09 2019-09-24 Range Fuels Inc "método para a produção de gás de síntese, método de formação de gás de síntese, método de produão de um produto, aparelho, método de desvalorização de um material de partida que contém carbono e aparelho para a produção de gás síntese"
US8142530B2 (en) 2007-07-09 2012-03-27 Range Fuels, Inc. Methods and apparatus for producing syngas and alcohols
US8236071B2 (en) 2007-08-15 2012-08-07 General Electric Company Methods and apparatus for cooling syngas within a gasifier system
US9074152B2 (en) 2007-09-12 2015-07-07 General Electric Company Plasma-assisted waste gasification system
WO2009049063A1 (fr) 2007-10-09 2009-04-16 Silvagas Corporation Systèmes et procédés pour l'oxydation de goudrons de gaz de synthèse
US8328889B2 (en) * 2007-12-12 2012-12-11 Kellogg Brown & Root Llc Efficiency of gasification processes
US7932298B2 (en) 2007-12-13 2011-04-26 Gyco, Inc. Method and apparatus for reducing CO2 in a stream by conversion to a syngas for production of energy
US7923476B2 (en) 2007-12-13 2011-04-12 Gyco, Inc. Method and apparatus for reducing CO2 in a stream by conversion to a syngas for production of energy
DE102007062413B3 (de) * 2007-12-20 2009-09-10 Conera Process Solutions Gmbh Verfahren und Vorrichtung zur Wiederaufbereitung von CO2-haltigen Abgasen
AU2009218694B2 (en) 2008-02-28 2014-02-13 Krones Ag Method and device for converting carbonaceous raw materials
ATE534744T1 (de) 2008-03-11 2011-12-15 Ineos Bio Ltd Verfahren zur herstellung von ethanol
DE102008027858A1 (de) 2008-06-11 2009-12-17 Jörg HO Verfahren und Vorrichtung zur Erzeugung eines teerfreien Brenngases
JP5282455B2 (ja) * 2008-06-17 2013-09-04 株式会社Ｉｈｉ ガス化ガスの改質方法及び装置
US8592190B2 (en) 2009-06-11 2013-11-26 Ineos Bio Limited Methods for sequestering carbon dioxide into alcohols via gasification fermentation
CA2727827C (fr) 2008-06-25 2015-04-28 Nexterra Systems Corp. Production de gaz de synthese propre a partir d'une biomasse
US8192647B2 (en) 2008-12-19 2012-06-05 Enerkem Inc. Production of synthesis gas through controlled oxidation of biomass
TW201026395A (en) * 2008-12-24 2010-07-16 Conocophillips Co Tar-free gasification system and process
US8357216B2 (en) * 2009-04-01 2013-01-22 Phillips 66 Company Two stage dry feed gasification system and process
US20100256246A1 (en) 2009-04-06 2010-10-07 Rentech, Inc. System and method for conditioning biomass-derived synthesis gas
US20100270505A1 (en) * 2009-04-22 2010-10-28 Range Fuels, Inc. Integrated, high-efficiency processes for biomass conversion to synthesis gas
US20100294179A1 (en) * 2009-05-18 2010-11-25 Covanta Energy Corporation Gasification combustion system
JP5400505B2 (ja) * 2009-07-06 2014-01-29 バブコック日立株式会社 コークス炉ガスの無触媒改質方法及び改質装置
US8764857B2 (en) * 2009-07-29 2014-07-01 All Power Labs, Inc. System and method for downdraft gasification
US8759047B2 (en) * 2009-09-16 2014-06-24 Coskata, Inc. Process for fermentation of syngas from indirect gasification
US8597934B2 (en) * 2009-10-30 2013-12-03 Coskata, Inc. Process for controlling sulfur in a fermentation syngas feed stream
MY150967A (en) * 2010-03-01 2014-03-31 Plascoenergy Ip Holdings Slb Carbon conversion system with integrated processing zones
US8999021B2 (en) 2010-04-13 2015-04-07 Ineos Usa Llc Methods for gasification of carbonaceous materials
US8580152B2 (en) 2010-04-13 2013-11-12 Ineos Usa Llc Methods for gasification of carbonaceous materials
US8585789B2 (en) 2010-04-13 2013-11-19 Ineos Usa Llc Methods for gasification of carbonaceous materials
US8691115B2 (en) * 2010-04-29 2014-04-08 Indiana University Research And Technology Corporation System and method for controlling char in biomass reactors
US8377154B2 (en) * 2010-05-18 2013-02-19 Kellogg Brown & Root Llc Gasification system and process for maximizing production of syngas and syngas-derived products
CN201713504U (zh) * 2010-05-24 2011-01-19 中国科学院广州能源研究所 一种生物质复合气化装置
CN101906339A (zh) * 2010-08-05 2010-12-08 中国石油大学(北京) 煤气化和甲烷化一体化生产代用天然气的工艺及装置
US20120255301A1 (en) 2011-04-06 2012-10-11 Bell Peter S System for generating power from a syngas fermentation process

Patent Citations (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4805561A (en) * 1987-12-11 1989-02-21 Shell Oil Company Coal gasification process with inhibition of quench zone plugging
EP0416242A1 (fr) * 1989-09-07 1991-03-13 Krupp Koppers GmbH Installation pour la production d'un gaz à partir de solides carbonifères finement divisés
DE4035293C1 (fr) * 1990-11-07 1992-01-02 Metallgesellschaft Ag, 6000 Frankfurt, De
WO1993018341A1 (fr) 1992-03-05 1993-09-16 Technische Universiteit Delft Procede et appareil de combustion d'un materiau carbone
US6033447A (en) * 1997-06-25 2000-03-07 Eastman Chemical Company Start-up process for a gasification reactor
US5984998A (en) 1997-11-14 1999-11-16 American Iron And Steel Institute Method and apparatus for off-gas composition sensing
US6435139B1 (en) 2000-12-14 2002-08-20 Borsig Gmbh Waste heat boiler for cooling hot syngas
WO2003060480A1 (fr) 2002-01-17 2003-07-24 L'air Liquide - Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et appareil de surveillance en temps reel de gaz de carneau de fours
WO2006015660A1 (fr) 2004-08-12 2006-02-16 Sms Demag Ag Mesure sans contact des fumees par spectroscopie irtf sur des unites metallurgiques
US7587995B2 (en) 2005-11-03 2009-09-15 Babcock & Wilcox Power Generation Group, Inc. Radiant syngas cooler
US7552701B2 (en) 2006-05-16 2009-06-30 Shell Oil Company Boiler for making super heated steam and its use
US20100180503A1 (en) * 2008-01-29 2010-07-22 Mitsubishi Heavy Industries Ltd Starting method of coal gasifier and starting device therefor
WO2009154788A2 (fr) 2008-06-20 2009-12-23 Ineos Usa Llc Procédés de séquestration de dioxyde de carbone dans des alcools par gazéification et fermentation
US20100044643A1 (en) * 2008-08-22 2010-02-25 Hunton Energy Holdings, LLC Low NOx Gasification Startup System
US20100090166A1 (en) * 2008-10-08 2010-04-15 Fournier Guillaume Guy Michel Process to prepare a gas mixture of hydrogen and carbon monoxide

Also Published As

Publication number Publication date
WO2013147918A2 (fr) 2013-10-03
EA029848B1 (ru) 2018-05-31
AU2012375190B2 (en) 2015-09-03
KR101934688B1 (ko) 2019-01-03
CN103874750A (zh) 2014-06-18
ES2660963T3 (es) 2018-03-26
CA2832419A1 (fr) 2012-10-11
CN103874750B (zh) 2016-02-03
ZA201308266B (en) 2016-08-31
EP2694625A1 (fr) 2014-02-12
TW201249979A (en) 2012-12-16
TW201245435A (en) 2012-11-16
ZA201308265B (en) 2016-08-31
ZA201308269B (en) 2017-06-28
EA201370218A1 (ru) 2014-08-29
JP2014515774A (ja) 2014-07-03
JP6102007B2 (ja) 2017-03-29
CR20130574A (es) 2014-03-19
CA2832554C (fr) 2019-02-26
KR20140058420A (ko) 2014-05-14
EA201370217A1 (ru) 2014-08-29
EA027557B1 (ru) 2017-08-31
BR112013025724B1 (pt) 2019-04-09
US20150037229A1 (en) 2015-02-05
CN107880943A (zh) 2018-04-06
PL2694432T3 (pl) 2018-11-30
US20120256131A1 (en) 2012-10-11
EP2694432B1 (fr) 2018-06-06
PL2694625T3 (pl) 2018-04-30
KR20180088920A (ko) 2018-08-07
BR112013025722B1 (pt) 2020-10-27
US20120256128A1 (en) 2012-10-11
JP2014514416A (ja) 2014-06-19
EP3301143A1 (fr) 2018-04-04
US9051523B2 (en) 2015-06-09
NZ617115A (en) 2015-09-25
TWI541337B (zh) 2016-07-11
TWI586922B (zh) 2017-06-11
PL2694624T3 (pl) 2019-07-31
JP6127323B2 (ja) 2017-05-17
AR085863A1 (es) 2013-10-30
TW201247862A (en) 2012-12-01
AU2012240302A1 (en) 2013-11-14
EP3556828A1 (fr) 2019-10-23
AR085866A1 (es) 2013-10-30
EP3381997A1 (fr) 2018-10-03
US10487280B2 (en) 2019-11-26
AU2012240302B2 (en) 2017-04-13
CN108611124B (zh) 2021-07-20
US8894885B2 (en) 2014-11-25
EP2694626A2 (fr) 2014-02-12
BR112013025724A2 (pt) 2018-07-24
JP6483733B2 (ja) 2019-03-13
EP2694626B1 (fr) 2018-06-13
ZA201308267B (en) 2016-08-31
CA2832431A1 (fr) 2013-03-07
US9028571B2 (en) 2015-05-12
CA2832419C (fr) 2021-05-04
JP2017101252A (ja) 2017-06-08
CN103874749B (zh) 2017-05-17
CA2832554A1 (fr) 2013-10-03
KR20190006025A (ko) 2019-01-16
NZ617114A (en) 2015-12-24
CN103874751A (zh) 2014-06-18
CN104039935A (zh) 2014-09-10
BR112013025718B1 (pt) 2019-12-10
MX2013011571A (es) 2014-01-17
EP3453747A1 (fr) 2019-03-13
ES2708221T3 (es) 2019-04-09
US20120256130A1 (en) 2012-10-11
AU2012375190A1 (en) 2013-11-14
EA201370215A1 (ru) 2014-08-29
EP2694625B1 (fr) 2017-11-15
CN103874751B (zh) 2016-06-22
AR085864A1 (es) 2013-10-30
EA201370216A1 (ru) 2014-08-29
KR101959702B1 (ko) 2019-03-18
EA027587B1 (ru) 2017-08-31
ZA201308271B (en) 2020-05-27
WO2012138751A1 (fr) 2012-10-11
EP2694432A2 (fr) 2014-02-12
CN108611124A (zh) 2018-10-02
BR112013025727A2 (pt) 2018-05-02
JP6415320B2 (ja) 2018-10-31
US9045706B2 (en) 2015-06-02
WO2012138766A2 (fr) 2012-10-11
AU2012240219B2 (en) 2016-07-28
CA2832434C (fr) 2020-06-30
AU2012302236A1 (en) 2013-11-14
BR112013025718A2 (pt) 2018-06-19
TWI541338B (zh) 2016-07-11
AU2012240219A1 (en) 2013-11-14
US9745529B2 (en) 2017-08-29
MY195696A (en) 2023-02-05
ES2740002T3 (es) 2020-02-05
EP2694624A1 (fr) 2014-02-12
EP2694623A1 (fr) 2014-02-12
CA3035043A1 (fr) 2013-03-07
NZ710264A (en) 2017-04-28
MY181501A (en) 2020-12-24
AU2012302236B2 (en) 2016-11-03
BR112013025722A2 (pt) 2018-04-24
WO2012138766A3 (fr) 2013-03-21
MX2013011570A (es) 2014-03-05
EP2694623B1 (fr) 2017-12-06
KR20140058421A (ko) 2014-05-14
MY172095A (en) 2019-11-13
EP3301143B1 (fr) 2019-06-12
KR20140056165A (ko) 2014-05-09
WO2012138762A1 (fr) 2012-10-11
TWI537375B (zh) 2016-06-11
US20200017784A1 (en) 2020-01-16
ES2686289T3 (es) 2018-10-17
PL3301143T3 (pl) 2019-12-31
CR20130575A (es) 2014-03-13
TW201248085A (en) 2012-12-01
KR101884494B1 (ko) 2018-08-01
MY188922A (en) 2022-01-13
JP6129818B2 (ja) 2017-05-17
WO2013147918A3 (fr) 2013-11-28
EP3381997B1 (fr) 2020-06-03
KR102026047B1 (ko) 2019-09-27
US20140246626A1 (en) 2014-09-04
JP2014512435A (ja) 2014-05-22
JP2017133013A (ja) 2017-08-03
RU2013149044A (ru) 2015-05-20
MX354778B (es) 2018-03-21
US20150232771A1 (en) 2015-08-20
CA2832434A1 (fr) 2012-10-11
CN103958649A (zh) 2014-07-30
PL2694623T3 (pl) 2018-05-30
TWI541339B (zh) 2016-07-11
CN103874749A (zh) 2014-06-18
CR20130573A (es) 2014-03-13
ES2656948T3 (es) 2018-03-01
US20120256129A1 (en) 2012-10-11
CR20130576A (es) 2014-03-13
US20120255301A1 (en) 2012-10-11
AR085932A1 (es) 2013-11-06
JP6698561B2 (ja) 2020-05-27
KR101882544B1 (ko) 2018-07-26
MY166661A (en) 2018-07-18
MX2013011708A (es) 2014-04-25
MX2013011567A (es) 2013-11-01
NZ617028A (en) 2015-09-25
KR101959581B1 (ko) 2019-03-18
CA2832431C (fr) 2019-04-23
BR112013025727B1 (pt) 2020-10-27
EA027586B1 (ru) 2017-08-31
CA3035043C (fr) 2021-07-13
EP2694624B1 (fr) 2018-10-31
TW201245436A (en) 2012-11-16
BR112013025720B1 (pt) 2021-11-30
BR112013025720A2 (pt) 2018-05-02
KR20140061312A (ko) 2014-05-21
JP2014510189A (ja) 2014-04-24
RU2603663C2 (ru) 2016-11-27
CN105907423A (zh) 2016-08-31
NZ617148A (en) 2015-09-25

Similar Documents

Publication Publication Date Title
US9045706B2 (en) Method of operation of process to produce syngas from carbonaceous material
NZ617115B2 (en) Method of operation of process to produce syngas from carbonaceous material
NZ617114B2 (en) Apparatus and methods for tar removal from syngas

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 12715788

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2014503951

Country of ref document: JP

Kind code of ref document: A

Ref document number: 2832431

Country of ref document: CA

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: MX/A/2013/011708

Country of ref document: MX

WWE Wipo information: entry into national phase

Ref document number: 2012715788

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 20137029101

Country of ref document: KR

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: 201370217

Country of ref document: EA

WWE Wipo information: entry into national phase

Ref document number: CR2013-000575

Country of ref document: CR

ENP Entry into the national phase

Ref document number: 2012302236

Country of ref document: AU

Date of ref document: 20120404

Kind code of ref document: A

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112013025718

Country of ref document: BR

ENP Entry into the national phase

Ref document number: 112013025718

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20131004